Saudi Arabian Oil Company

Sabic Global Technologies B.v.

King Fahd University of Petroleum and Minerals

Saudi Basic Industries Corporation

Mian Rahat Saeed

Musaed Salem Al-Ghrami

Abdullah Mohammed Aitani

Mansour Ali Al-Herz

Mohammed Abdul Bari Siddiqui

Nabil Al-Yassir

Ahmed Alzenaidi

Vidya Sagar Guggilla

Rabindran Jermy Balasamy

Mohammed A Siddiqui

Sulaiman Saleh Al-Khattaf

Fahad A Al-Sherehy

Mohammad Akhtar Zahoor

Sulaiman S Al-khattaf

Olagoke Olabisi

Mohammed M Abdillahi

The presently disclosed subject matter relates to methods of producing ethylene and propylene by the catalytic steam cracking of naphtha using an HZSM-5 catalyst. An example method can include providing a naphtha feedstock, providing steam, and providing an HZSM-5 catalyst. The method can further include preparing the HZSM-5 catalyst by titanium modification or alkaline treatment, followed by phosphorus modification. The method can further include feeding the naphtha feedstock and steam to a reactor containing the catalyst and removing an effluent from the reactor having a combined yield of ethylene and propylene of greater than about 45 wt-%.

Methods for producing ethylene and propylene from naphtha

Provided here are zirconium-substituted hierarchical zeolite compositions and methods of preparing such catalytic compositions. One such method involves subjecting the zirconium-substituted zeolite to a framework modification process using a single template to produce a framework-modified zeolite, followed by subjecting the framework-modified zeolite to an ion exchange process to produce a hierarchical zeolite composition. Also provided are methods of catalytic cracking of hydrocarbon feedstocks using these zirconium-substituted hierarchical zeolite compositions.

Methods for synthesizing hierarchical zeolites for catalytic cracking

A catalyst and a process are provided for oligomerizing ethylene. A heterogeneous catalyst system comprises: (1) a chelating ligand, preferably 2-diphenyl phosphino benzoic acid (DPPBA); (2) a nickel precursor, preferably nickel chloride hexahydrate (NiCl,.6H,O); (3) a catalyst activator, preferably sodium tetraphenylborate (NaBPh,); and (4) silica. A 1:1:1 molar ratio of Ni:DPPBA:BPh,catalyst components are fixed on a silica support using low-temperature fixation. The catalyst components are dispersed in a diluent, preferably ethanol, and silica is added. The ethanol is evaporated using freeze-drying equipment to form a silica-supported catalyst system. The silica-supported catalyst is slurried in ethanol in a reactor, and ethylene is added. The reactor pressure and temperature are maintained at about 725 psig and 100&deg; C., respectively, for about two hours. The oligomer product formed has a narrower weight percent distribution, typically having about 96 weight percent C,'s to C,'s, compared to product formed using a homogeneous catalyst system.

Catalyst and process for ethylene oligomerization

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Dhahran, Saudi Arabia

Mian Rahat Saeed